化工学报 ›› 2022, Vol. 73 ›› Issue (5): 2031-2038.DOI: 10.11949/0438-1157.20220036
收稿日期:
2022-01-07
修回日期:
2022-02-09
出版日期:
2022-05-05
发布日期:
2022-05-24
通讯作者:
贾胜坤,袁希钢
作者简介:
刘星伟(1997—),男,硕士研究生,基金资助:
Xingwei LIU1(),Shengkun JIA1(),Yiqing LUO1,Xigang YUAN1,2()
Received:
2022-01-07
Revised:
2022-02-09
Online:
2022-05-05
Published:
2022-05-24
Contact:
Shengkun JIA,Xigang YUAN
摘要:
从结构优化角度建立精馏塔优化的混合整数非线性规划(MINLP)模型,为了消除整数变量,引入绕流效率将MINLP问题转化为非线性规划(NLP)问题。针对得到的NLP问题提出一种优化方法,在该方法中采用结构优化中常用的信赖域优化算法进行求解,并应用虚拟瞬态连续性方程辅助优化中的稳态模拟。采用提出的优化方法对3个精馏系统进行设计优化,以不同初始值开始,均可得到令人满意的优化结果,表明所提优化方法具有良好的稳健性,对于较复杂的部分热耦合精馏过程仍然可以有效优化求解;信赖域算法在精馏塔优化中也表现出良好的收敛性。
中图分类号:
刘星伟, 贾胜坤, 罗祎青, 袁希钢. 基于信赖域算法的精馏塔优化[J]. 化工学报, 2022, 73(5): 2031-2038.
Xingwei LIU, Shengkun JIA, Yiqing LUO, Xigang YUAN. Optimization of distillation column based on trust region algorithm[J]. CIESC Journal, 2022, 73(5): 2031-2038.
绕流效率的 初值 | N1 | N2 | RR/ (kmol/kmol) | Vf/ (kmol/kmol) | TAC/ (104 USD/a) |
---|---|---|---|---|---|
0.1 | 20 | 19 | 6.30 | 0.8348 | 325.445 |
0.3 | 20 | 19 | 6.30 | 0.8348 | 325.445 |
0.5 | 21 | 20 | 6.15 | 0.8323 | 327.789 |
0.7 | 20 | 20 | 6.22 | 0.8334 | 326.351 |
0.9 | 21 | 20 | 6.15 | 0.8323 | 327.789 |
表1 乙苯-苯乙烯分离塔的优化结果
Table 1 Optimization results of ethylbenzene-styrene column
绕流效率的 初值 | N1 | N2 | RR/ (kmol/kmol) | Vf/ (kmol/kmol) | TAC/ (104 USD/a) |
---|---|---|---|---|---|
0.1 | 20 | 19 | 6.30 | 0.8348 | 325.445 |
0.3 | 20 | 19 | 6.30 | 0.8348 | 325.445 |
0.5 | 21 | 20 | 6.15 | 0.8323 | 327.789 |
0.7 | 20 | 20 | 6.22 | 0.8334 | 326.351 |
0.9 | 21 | 20 | 6.15 | 0.8323 | 327.789 |
绕流效率的初始值 | N1 | N2 | N3 | N4 | RR1/(kmol/kmol) | Vf1/(kmol/kmol) | RR2/(kmol/kmol) | Vf2/(kmol/kmol) | TAC/(104 USD/a) |
---|---|---|---|---|---|---|---|---|---|
0.1 | 9 | 14 | 12 | 13 | 1.41 | 0.6124 | 1.50 | 0.7535 | 544.851 |
0.3 | 8 | 15 | 11 | 12 | 1.42 | 0.6142 | 1.52 | 0.7551 | 544.371 |
0.5 | 8 | 14 | 11 | 12 | 1.44 | 0.6142 | 1.53 | 0.7555 | 544.024 |
0.7 | 8 | 14 | 12 | 12 | 1.43 | 0.6137 | 1.52 | 0.7546 | 544.207 |
0.9 | 8 | 14 | 11 | 12 | 1.44 | 0.6142 | 1.53 | 0.7556 | 544.024 |
表2 直接序列精馏塔的优化结果
Table 2 Optimization results of direct sequence distillation column
绕流效率的初始值 | N1 | N2 | N3 | N4 | RR1/(kmol/kmol) | Vf1/(kmol/kmol) | RR2/(kmol/kmol) | Vf2/(kmol/kmol) | TAC/(104 USD/a) |
---|---|---|---|---|---|---|---|---|---|
0.1 | 9 | 14 | 12 | 13 | 1.41 | 0.6124 | 1.50 | 0.7535 | 544.851 |
0.3 | 8 | 15 | 11 | 12 | 1.42 | 0.6142 | 1.52 | 0.7551 | 544.371 |
0.5 | 8 | 14 | 11 | 12 | 1.44 | 0.6142 | 1.53 | 0.7555 | 544.024 |
0.7 | 8 | 14 | 12 | 12 | 1.43 | 0.6137 | 1.52 | 0.7546 | 544.207 |
0.9 | 8 | 14 | 11 | 12 | 1.44 | 0.6142 | 1.53 | 0.7556 | 544.024 |
绕流效率的初始值 | N1 | N2 | N3 | N4 | RR1/(kmol/kmol) | Sf/(kmol/kmol) | RR2/(kmol/kmol) | Vf/(kmol/kmol) | TAC/(104 USD/a) |
---|---|---|---|---|---|---|---|---|---|
0.1 | 8 | 17 | 11 | 11 | 2.53 | 0.4507 | 2.53 | 0.6611 | 224.098 |
0.3 | 7 | 17 | 11 | 11 | 2.56 | 0.4476 | 2.52 | 0.6620 | 224.189 |
0.5 | 7 | 18 | 10 | 11 | 2.56 | 0.4485 | 2.54 | 0.6631 | 224.328 |
0.7 | 8 | 18 | 11 | 11 | 2.51 | 0.4508 | 2.52 | 0.6605 | 224.206 |
0.9 | 7 | 18 | 10 | 11 | 2.56 | 0.4485 | 2.54 | 0.6631 | 224.328 |
表3 部分热耦合精馏过程优化结果
Table 3 Optimization results of partially thermally coupled distillation process
绕流效率的初始值 | N1 | N2 | N3 | N4 | RR1/(kmol/kmol) | Sf/(kmol/kmol) | RR2/(kmol/kmol) | Vf/(kmol/kmol) | TAC/(104 USD/a) |
---|---|---|---|---|---|---|---|---|---|
0.1 | 8 | 17 | 11 | 11 | 2.53 | 0.4507 | 2.53 | 0.6611 | 224.098 |
0.3 | 7 | 17 | 11 | 11 | 2.56 | 0.4476 | 2.52 | 0.6620 | 224.189 |
0.5 | 7 | 18 | 10 | 11 | 2.56 | 0.4485 | 2.54 | 0.6631 | 224.328 |
0.7 | 8 | 18 | 11 | 11 | 2.51 | 0.4508 | 2.52 | 0.6605 | 224.206 |
0.9 | 7 | 18 | 10 | 11 | 2.56 | 0.4485 | 2.54 | 0.6631 | 224.328 |
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